Hydrocarbon conversion with a sulfided bimetallic catalytic composite

ABSTRACT

Hydrocarbons are converted by contacting them at hydrocarbon conversion conditions with a sulfided bimetallic acidic catalytic composite comprising a combination of catalytically effective amounts of a platinum group component, a sulfur component, a bismuth component and a halogen component with a porous carrier material. The platinum group component, sulfur component, and halogen component are present in the bimetallic catalyst in amounts respectively, calculated on an elemental basis, corresponding to about 0.01 to about 2 wt. % platinum group metal, about 0.05 to about 1 wt. % sulfur and about 0.1 to about 3.5 wt. % halogen. The bismuth component is present in amounts corresponding to an atomic ratio of bismuth to platinum group metal of about 0.1:1 to about 1:1. Moreover, these metallic components are uniformly dispersed throughout the porous carrier material in carefully controlled oxidation states such that substantially all of the platinum group metal and bismuth components are present therein in the corresponding elemental metallic states while substantially all the sulfur component is present therein in the form of physically adsorbed or chemisorbed sulfide. A specific example of the type of hydrocarbon conversion process disclosed is a process for the catalytic reforming of a low-octane gasoline fraction wherein the gasoline fraction and hydrogen stream are contacted with the novel sulfided bimetallic catalyst disclosed herein at reforming conditions.

United States Patent 1 Wilhelm 1 June 10, 1975 [75] Inventor: Frederick C. Wilhelm, Arlington Heights, 111.

[73] Assignee: Universal Oil Products Company, Des Plaines, 111.

[22] Filed: Feb. 11, 1974 [21] Appl. No.2 441,198

Related US. Application Data [63] Continuation-in-part of Ser. No. 233,819, March 10,

1972, Pat. NO. 3,798,155.

[52] US. Cl 208/139; 252/439 [51] Int. Cl ClOg 35/08; BOlj 11/74 [58] Field of Search 208/138, 139, 111; 252/439, 441; 260/683.68

[56] References Cited UNITED STATES PATENTS 2,245,735 6/1941 Subkow 260/683.58 3,156,737 ll/1964 Gutberlet 260/683.65 3,206,391 9/1965 Cutberlet et al 208/108 3,291,755 12/1966 Haensel et a1. 260/6833 3,442,796 5/1969 Hayes 208/139 3,511,888 5/1970 Jenkins 208/138 3,651,162 3/1972 Pohlmann et a1. 260/672 T 3,651,163 3/1972 Redford et a1 208/139 3,786,001 1/1974 Cornelius 252/464 Primary ExaminerDelbert E. Gantz Assistant Examiner-James W. Hellwege Attorney, Agent, or FirmJames R. Hoatson, .lr.; Thomas K. McBride; William H. Page, II

[5 7] ABSTRACT Hydrocarbons are converted by contacting them at hydrocarbon conversion conditions with a sulfided bimetallic acidic catalytic composite comprising a combination of catalytically effective amounts of a platinum group component, a sulfur component, a bismuth component and a halogen component with a porous carrier material. The platinum group component, sulfur component, and halogen component are present in the bimetallic catalyst in amounts respectively, calculated on an elemental basis, corresponding to about 0.01 to about 2 wt. platinum group metal, about 0.05 to about 1 wt. sulfur and about 0.1 to about 3.5 wt. halogen. The bismuth component is present in amounts corresponding to an atomic ratio of bismuth to platinum group metal of about 0.1:1 to about 1:1. Moreover, these metallic components are uniformly dispersed throughout the porous carrier material in carefully controlled oxidation states such that substantially all of the platinum group metal and bismuth components are present therein in the corresponding elementalmetallic states while substantially all the sulfur component is present therein in the form of physically adsorbed or chemisorbed sulfide. A specific example of the type of hydrocarbon conversion process disclosed is a process for the catalytic reforming of a low-octane gasoline fraction wherein the gasoline fraction and hydrogen stream are contacted with the novel sulfided bimetallic catalyst disclosed herein at reforming conditions.

13 Claims, No Drawings HYDROCARBON CONVERSION WITH A SULFIDED BIMETALLIC CATALYTIC COMPOSITE CROSS-REFERENCES TO RELATED APPLICATIONS This application is a continuation-in-part of my prior, application Ser. No. 233,819 filed Mar. 10, 1972, now US. Pat. No. 3,798,155 all of the teachings of which are specifically incorporated herein by reference.

The subject of the present invention is a novel acidic sulfided bimetallic catalytic composite which has exceptional activity, selectivity and resistance to deactivation when employed in a hydrocarbon conversion process that requires a catalyst having both a hydrogenation-dehydrogenation function and a selec tive acid or cracking function. More precisely, the present invention involves a novel sulfided dual-function acidic bimetallic catalytic composite which beneficially utilizes a catalytic component, bismuth, which traditionally has been thought of and taught to be a poison for a platinum group metal because of its close proximity in the Periodic Table to the notorious platinum poison, arsenic. Bismuth is utilized in the present invention to interact with a platinum group metaland sulfurcontaining acidic catalyst to enable substantial improvements in hydrocarbon conversion processes of the type that have traditionally utilized platinum group metal-containing catalysts to accelerate the various hydrocarbon conversion reactions associated therewith In another aspect this invention concerns the improved processes that are produced by the use of a sulfided acidic bimetallic catalytic composite comprising a combination of a platinum group component, a sulfur component, a bismuth component, and a halogen component with a porous, high surface area carrier material in a manner such that 1 the platinum group and bismuth components are uniformly dispersed throughout the porous carrier material, (2) the amount of the bismuth component is not greater than the amount of the platinum group component on an atomic basis, and (3) substantially all of the platinum group and bismuth components are present therein as the corresponding metals while substantially all of the sulfur component is present therein in the form of physically adsorbed or chemisorbed sulfide. In a specific aspect, the present invention concerns an improved reforming process which utilizes the subject sulfided acidic bimetallic catalyst to markedly improve activity, selectivity and stability characteristics associated therewith, to increase yields of C reformate and of hydrogen recovered therefrom and to allow operation thereof at high severity conditions not heretofore generally employed in the art of continuous catalytic reforming of hydrocarbons with a platinum-containing monometallic, dualfunction catalyst.

Composites having a hydrogenationdehydrogenation function and a selective acid or cracking function are widely used today as catalysts in many industries, such as the petroleum or petrochemical industry, to accelerate a wide spectrum of hydrocarbon conversion reactions. Generally, the cracking function is thought to be associated with an acid-acting material of the porous, adsorptive, refractory oxide type which is typically utilized the support or carrier for a heavy metallic component such as the metals or compounds of metals of the transition elements of Groups V through VIII of the Periodic Table to which are generally attributed the hydrogenationdehydrogenation function.

These catalytic composites are used to accelerate a wide variety of hydrocarbon conversion reactions such as hydrocracking, isomerization, dehydrogenation, hydrogenation, desulfurization, cyclization, alkylation, polymerization, halogenation, hydrogenolysis, cracking, hydroisomerization, etc. In many cases, the commercial applications of these catalysts are in processes where more than one of these reactions are proceeding simultaneously. An example of this type of process is reforming wherein a hydrocarbon feed stream containing paraffins and naphthenes is subjected to conditions which promote dehydrogenation of naphthenes to aromatics, dehydrocyclization of paraffins to aromatics, isomerization of paraffins and naphthenes, hydrocracking of naphthenes and paraffins, and the like reactions to produce an octane-rich or aromatic-rich product stream. Another example is a hydrocracking process wherein catalysts of this type are utilized to effect selective hydrogenation and cracking of high molecular weight unsaturated materials, selective hydrocracking of high molecular weight materials, and other like reactions, to produce a generally lower boiling, more valuable output stream. Yet another example is a hydroisomerization process wherein a hydrocarbon fraction which is relatively rich in straight-chain paraffin and/or olefinic compounds are contacted with a dual-function catalyst to produce an output stream rich in isoparaffin compounds.

Regardless of the reaction involved or the particular process involved, it is of critical importance that the dual-function catalyst exhibit not only the capability to initially perform its specified functions but also that it has the capability to perform them satisfactorily for prolonged periods of time. The analytical terms used in the art to measure how well a particular catalyst performs its intended functions in a particular hydrocarbon reaction environment are activity, selectivity and stability. And for purposes of discussion here these terms are conveniently defined for a given charge stock as follows: (1) activity is a measure of the catalysts ability to convert hydrocarbon reactants into products at a specified severity level where severity level means the reaction conditions used that is, the temperature, pressure, contact time, and pressure of diluents such as H (2) selectivity refers to the amount of desired product or products obtained relative to the amount of reactants converted or charged; (3) stability refers to the rate of change with time of the activity and selectivity parameters obviously, the smaller rate implying the more stable catalyst. In a reforming process, for example, activity commonly refers to the amount of conversion that takes place for a given charge stock at a specified severity level and is typically measured by octane number of the (7 product stream; selectivity usually refers to the amount of (1 yield that is obtained at the particular severity or activity level relative to the amount of the charge stock; and stability is typically equated to the rate of change with time of activity, as measured by octane number of C product and of selectivity, as measured by (3 yield. Actually, this last statement is not strictly correct because generally a continuous reforming process is run to produce a constant octane C product with a severity level being continuously adjusted to attain this result; and, furthermore, the severity level is for this process usually varied by adjusting the conversion temperature in the reaction zone so that, in point of fact, the rate of change of activity finds response in the rate of change of conversion temperatures and changes in this last parameter are customarily taken as indicative of activity stability.

As is well known to those skilled in the art, the principal cause of observed deactivation or instability of a dual-function catalyst when it is used in a hydrocarbon conversion reaction is associated with the fact that coke forms on the surface of the catalyst during the course of the reaction. More specifically, in these hydrocarbon conversion processes, the conditions utilized typically result in the formation of heavy, high molecular weight, black, solid or semisolid, carbonaceous material which coats the surface of the catalyst and reduces its activity by shielding its active sites from the reactants. in other words, the performance of this dualfunction catalyst is sensitive to the presence of carbonaceous deposits on the surface of the catalyst. Accordingly, the major problem facing workers in this area of the art is the development of more active and selective catalytic composites that are not as sensitive to the presence of these carbonaceous materials and/or have the capability to suppress the rate of formation of these carbonaceous materials on the catalyst. Viewed in terms of performance parameters, the problem is to develop a dual-function catalyst having superior activity, selectivity and stability. In particular, for a reforming process the problem is typically expressed in terms of shifting and stabilizing the C yield-octane relationship C yield being representative of selectivity and octane being proportional to activity.

I have now found a dual-function catalytic composite which possesses improved activity, selectivity and stability when it is employed in a process for the conversion of hydrocarbons of the type which have heretofore utilized dual-function catalytic composites such as pro cesses for isomerization, hydroisomerization, dehydrogenation, desulfurization, denitrogenization, hydrogenation, alkylation, dealkylation, disproportionation,

polymerization, oligomerization, hydrodealkylation, transalkylation, cyclization, dehydrocyclization, cracking, hydrocracking, reforming, hydrogenation, halogenation, and the like processes. In particular, I have as certained that a sulfided acidic bimetallic catalytic composite, comprising a combination of a platinum group component, a bismuth component, a sulfur component and a halogen component with a porous refractory carrier material. can enable the performance of a hydrocarbon conversion process utilizing a dualfunction catalyst to be substantially improved, provided the amounts and oxidation states of the metallic compounds and the distribution thereof in the catalytic composite are carefully controlled in the manner indicated herein. Since the earliest introduction of catalysts containing a platinum group component, it has been axiomatic that the effect of arsenic on a platinumcontaining catalyst is detrimental. This concept has become so fixed and certain in the art that tremendous efforts have been devoted to removing arsenic contaminants from charge stocks that are to be processed in a unit containing a platinum catalyst. In addition, the art is replete with a significant number of methods for re activating a platinum-containing catalyst once it has been deactivated by contact with arsenic or compounds of arsenic. Because bismuth is a member of the same group of the Periodic Table (Group VA) and is known to have similar chemical properties to arsenic, it has fallen into the same category and has been traditionally thought of as a poison for a platinumcontaining catalyst. The art has on occasion hinted at or proposed to use the poisoning effect of Group VA metallic elements to modify or attenuate the platinum component of a dual-function catalyst. For examples of these suggestions, reference may be had to the teachings of US. Pat. Nos. 3,156,737; 3,206,391; 3,291,755 and 3,511,888. However, the art has not recognized that bismuth can be utilized to promote a platinumcontaining catalyst; that is, to simultaneously increase its activity, selectivity and stability in hydrocarbon conversion service. In particular, the art has apparently never contemplated the use of a platinum-bismuth catalyst in a catalytic reforming process. As a matter of fact, the art on this last process is replete with teachings that contact of the platinumcontaining reforming catalyst, with metallic elements of Group VA of the Periodic Table, and particularly arsenic, is to be avoided if at all possible and if contact occurs to any substantial degree the catalyst must be immediately regenerated or reactivated by procedures for removal of these detrimental Group VA constituents. ln sharp contrast to this historic teaching of the art that bismuth is detrimental to a platinum-containing reforming catalyst, l have now discerned that the presence of bismuth in a catalyst containing a platinum group component and a sulfur component can be very beneficial under certain conditions. One essential condition associated with the acquisition of the beneficial aspects of bismuth with this type of platinum-containing catalyst is the atomic ratio of bismuth to platinum group metal contained in the composite; my findings here indicate that it is only when this ratio is not greater than 1:1 that the beneficial interaction of bismuth with a platinum metal is obtained. A second condition is the presence of a halogen component; my finding on this matter is that the presence of a relatively small amount of halogen is required to see the beneficial effect. Another condition for achieving this beneficial interaction of bismuth with this type of catalyst is the destribution of the bismuth and the platinum group metal components in the carrier material with which they are combined; my finding here is that it is essential that these components be uniformly dispersed throughout the porous carrier material that is, the concentration of these components is approximately the same in any reasonably divisible portion thereof. Still another condition for this beneficial effect is the oxidation states of the components; my finding here is that it is essential that the bismuth and platinum group metal are present in the composite in the corresponding elemental metallic states while the sulfur component is present therein in the form of physically adsorbed or chemisorbed sulfide. A sulfided bimetallic acidic catalyst meeting these essential limitations differs sharply both in substance and in capabilities from the bismuthand platinum-containin g catalyst that are suggested by the prior art.

In the case of a reforming process, one of the principal advantages associated with the use of the instant sulfided acidic bimetallic catalyst involves the acquisition of the capability to operate in a stable manner in a high severity operation; for example, a continuous reforming process producing a (1 reformate having an octane of about F-l clear and utilizing a'relatively low pressure of 50 to about 350 psig. In this latter embodiment the principal effect of the bismuth component is to stabilize the platinum group component by providing a mechanism for allowing it to better resist the rather severe deactivation normally associated with these conditions. ln short, the present invention essentially involves the finding that the addition of a controlled amount of a bismuth component to a dualfunction hydrocarbon conversion catalyst, containing a platinum group component, a sulfur component and a halogen component. coupled with the uniform distribution of the bismuth component throughout the catalytic composite to achieve an atomic ratio of bismuth to platinum group metal of not greater than 1:1 and with careful control of the oxidation states of the metallic components enables the performance characteristics of the catalyst to be sharply and materially improved.

It is, accordingly, one object of the present invention to provide a sulfided acidic bimetallic hydrocarbon conversion catalyst having superior performance characteristics when utilized in a hydrocarbon conversion process. A second object is to provide a sulfided acidic bimetallic catalyst havng dual-function hydrocarbon conversion performance characteristics that are relatively insensitive to the deposition of hydrocarbonaceous material thereon. A third object is to provide preferred methods of preparation of this bimetallic catalytic composite which insures the achievement and maintenance of its beneficial properties. Another object is to provide an improved reforming catalyst having superior activity, selectivity and stability when employed in a low pressure reforming process. Yet another object is to provide a dual-function hydrocarbon conversion catalyst which utilizes a relatively inexpensive component, bismuth, to promote and stabilize a platinum group metal component. Still another object is to provide a method of preparation of a bismuthcontaining bimetallic catalyst which insures the bismuth component is in a highly dispersed metallic state during use in the conversion of hydrocarbons.

In brief summary, the present invention is, in one embodiment a catalytic composite comprising a porous carrier material containing, on an elemental basis, about 0.01 to about 2 wt. platinum group metal, about 0.1 to about 3.5 wt. 70 halogen, about 0.05 to about 1 wt. sulfur and bismuth in an amount sufficient to result in an atomic ratio of bismuth to platinum group metal of about 0.1:] to about 1:1, wherein the platinum group metal and bismuth are uniformly dispersed throughout the porous carrier material, wherein substantially all of the platinum group metal and hismuth are present in the corresponding elemental metallic states and wherein substantially all of the sulfur is present therein in the form of physically adsorbed or chemisorbed sulfide.

A second embodiment relates to a catalytic composite comprising a porous carrier material containing, on an elemental basis, about 0.05 to about 1 wt. 7: platinum or palladium or iridium metal, about 0.5 to about 1.5 wt. halogen, about 0.05 to about 0.5 wt. sulfur, and bismuth in an amount sufficient to result in an atomic ratio of bismuth to platinum or palladium or iridium of about 0.1:1 to about 0.75:1, wherein substantially all of the platinum or palladium or iridium and bismuth are present in the corresponding elemental metallic states, wherein substantially all of the sulfur is present therein in the form of physically adsorbed or chemisorbed sulfide and wherein the metallic ingredients are uniformly dispersed in the porous carrier material.

Another embodiment relates to a process for the conversion of hydrocarbons comprising contacting the hydrocarbon and hydrogen with the catalytic composite described above in the first embodiment at hydrocarbon conversion conditions.

A preferred embodiment relates to a process for reforming a gasoline fraction which comprises contacting the gasoline fraction and hydrogen with the catalytic composite described above in the first embodiment at reforming conditions selected to produce a high-octane reformate. Other objects and embodiments of the present invention relate to additional details regarding preferred catalytic ingredients, preferred amounts of ingredients, suitable methods of composite preparation, operating conditions for use, in the hydrocarbon conversion pro cesses, and the like particulars which are herinafter given in the following detailed discussion of each of these facets of the present invention.

The sulfided acidic bimetallic catalyst of the present invention comprises a porous carrier material or support having combined therewith catalytically effective amounts of a platinum group component, a bismuth component, a sulfur component, and a halogen component.

Considering first the porous carrier material utilized in the present invention, it is preferred that the material be a porous, adsorptive, high-surface area support having a surface area of about 25 to about 500 m /g. The porous carrier material should be relatively refractory to the conditions utilized in the hydrocarbon conversion process, and it is intended to include within the scope of the present invention carrier materials which have traditionally been utilized in dual-function hydrocarbon conversion catalysts such as: (l activated carbon, coke or charcoal; (2) silica or silica gel, silicon carbide, clays and silicates including those synthetically-prepared and naturally-occurring, which may or may not be acid treated, for example, attapulgus clay, china clay, diatomaceous earth, fullers earth, kaoline, kieselguhr, etc.; (3) ceramics, porcelain, crushed firebrick, bauxite; (4) refractory inorganic oxides such as alumina, beryllium oxide, cerium oxide, titanium oxide, zirconium dioxide, chromium oxide, zinc oxide, hafnium oxide, magnesia, thoria, boria, vanadia, silicaalumina, silica-magnesia, chromia-alumina, aluminaboria, silica-zirconia, etc.; (5) zeolitic crystalline aluminosilicates such as naturally-occurring or syntheticallyprepared mordenite and/or faujasite, either in the hydrogen form or in a form which has been treated with multivalent cations; (6) spinels such as MgAl O FeAl- 0 ZnAl- O CaAl O,,, and other like compounds having the formula MO'Al O where M is a metal having a valence of 2; and (7) combinations of elements from one or more of these groups. The preferred porous carrier materials for use in the present invention are refractory inorganic oxides, with best results obtained with a carrier material consisting essentially of alumina, Suitable alumina materials are the crystalline aluminas known as the gamma-, etaand theta-alumina, with gammaor eta-alumina giving best results. In addition, in some embodiments the alumina carrier material may contain minor proportions of other well known refractory inorganic oxides such as silica, zirconia, magnesia,

etc.; however, the preferred support is substantially pure gammaor eta-alumina. Preferred carrier materials have an apparent bulk density of about 0.3 to about 0.7 g/cc and surface area characteristics such that the average pore diameter is about 20 to 300 Angstroms. the pore volume is about 0.1 to about 1 cc/g and the surface area is about 100 to about 500 m /g. In general. best results are typically obtained with a gammaalumina carrier material which is used in the form of spherical particles having: a relatively small diameter (i.e. typically about one-sixteenth inch). an apparent bulk density of about 0.5 to about 0.6 g/cc, a pore volume of about 0.4 cc/g, and a surface area of about l75 m /g.

The preferred alumina carrier material may be prepared in any suitable manner and may be syntheticallyprepared or natural occurring. Whatever type of alumina is employed it may be activated prior to use by one of more treatments including drying, calcination, steaming, etc., and it may be in a form known as activated alumina, activated alumina of commerce, porous alumina, alumina gel, etc. For example, the alumina carrier may be prepared by adding a suitable alkaline reagent, such as ammonium hydroxide, to a salt of aluminum such as aluminum chloride, aluminum nitrate, etc.; in an amount to form an aluminum hydroxide gel which upon drying and calcination is converted to alumina. The alumina carrier may be formed in any desired shape such as spheres, pills, cakes, extrudates, powders, granules, tablets, etc., and utilized in any desired size. For the purpose of the present invention a particularly preferred form of alumina is the sphere; and alumina spheres may be continuously manufactured by the well known oil drip method which comprises: forming an alumina hydrosol by any of the techniques taught in the art and preferably by reacting aluminum metal with hydrochloric acid, combining the resulting hydrosol with a suitable gelling agent and dropping the resultant mixture into an oil bath maintained at elevated temperatures. The droplets of the mixture remain in the oil bath until they set and form hydrogel spheres. The spheres are then continuously withdrawn from the oil bath and typically subjected to specific aging treatments in oil and an ammoniacal solution to further improve their physical characteristics. The re sulting aged and gelled particles are then washed and dried at a relatively low temperature of about 300 F. to about 400 F. and subjected to a calcination procedure at a temperature of about 850 to about 1300 F. for a period of about 1 to about 20 hours. This treatment effects conversion of the alumina hydrogel to the corresponding crystalline gammaalumina. See the teachings of U.S. Pat. No. 2,620,314 for additional details.

One ingredient of the subject catalyst is the platinum group component. That is, it is intended to cover the use of platinum or palladium or iridium or rhodium or osmium or ruthenium or mixtures thereof as a principal metallic component of the present composite. It is an essential feature of the present invention that substantially all of the platinum group component exists within the final catalytic composite in the elemental metallic state (i.e. as elemental platinum or palladium or iridium. etc.). Generally, the amount of the second component used in the final composite is relatively small compared to the amount of the other components combined therewith. in fact, the platinum group component generally will comprise about 0.01 to about 2 wt. of the final catalytic composite calculated on an elemental basis. Excellent results are obtained when the catalyst contains about 0.05 to about 1 wt. of platinum. iridium or palladium metal.

This platinum group component may be incorporated in the catalytic composite in any suitable manner known to result in a relatively uniform distribution of this component in the carrier material such as coprecipitation or cogellation, ion-exchange, or impregnation. The preferred method of preparing the catalyst involves the utilization of a soluble, decomposable compound of a platinum group metal to impregnate the carrier material in a relatively uniform manner. For example, this component may be added to the support by commingling the latter with an aqueous solution of chloroplatinic, chloroiridic or chloropalladic acid. Other water-soluble compounds of platinum group metals may be employed in impregnation solutions and include ammonium chloroplatinate, bromoplatinic acid, platinum dichloride, platinum tetrachloride hydrate, platinum dichlorocarbonyl dichloride, dinitrodiaminoplatinurn, tetrarnmine platinum chloride, palladium chloride, palladium nitrate, palladium sulfate, etc. The utilization of a platinum group metal chloride compound, such as chloroplatinic, chloroiridic or chloropalladic acid, is preferred since it facilitates the incorporation of both the platinum group component and at least a minor quantity of the halogen component in single step. Hydrogen chloride or the like acid is also generally added to the impregnation solution in order to further facilitate the incorporation of the halogen component and the uniform distribution of the metallic component throughout the carrier mate rial. In addition, it is generally preferred to impregnate the carrier material after it has been calcined in order to minimize the risk of washing away the valuable platinum or palladium compounds; however, in some cases it may be advantageous to impregnate the carrier material when it is in a gelled state.

A second essential constituent of the bimetallic composite of the present invention is a bismuth component. it is an essential feature of the present invention that substantially all of this component is present in the composite as the elemental metal. That is, it is believed to be a prerequisite for the acquisition of the beneficial effect of bismuth on a platinum-containin g catalyst that the bismuth component exists in the catalytic composite in the Zero oxidation state. All of the methods of preparation of the catalytic composite of the present invention include a substantially water-free, high temperature, prereduction step which is designed to result in the composite containing substantially all of the bismuth component in the elemental metallic state.

The bismuth component may be incorporated into the catalytic composite in any suitable manner known to effectively disperse this component throughout the carrier material or to result in this condition. Thus, this incorporation may be accomplished by coprecipitation or cogellation with the porous carrier material, ionexchange with the carrier material while it is in a gel state, or impregnation of the carrier material at any stage in its preparation. It is to be noted that it is intended to include within the scope of the present invention all conventional methods for incorporating a metallic component in a catalytic composite which results in a uniform distribution of the metallic component throughout the associated carrier material. One preferred method of incorporating the bismuth component into the catalytic composite involves coprecipitating the bismuth component during the preparation of the preferred refractory oxide carrier material. Typically, this involves the addition of a suitable, soluble, decomposable bismuth compound or complex to the alumina hydrosol, and then combining the hydrosol with a suitable gelling agent and dropping the resulting mixture into an oil bath as explained in detail hereinbefore. After drying and calcining the resulting gelled carrier material, there is obtained an intimate combination of alumina and bismuth oxide, which combination has the bismuth component uniformly dispersed throughout the alumina. Another preferred method of incorporating the bismuth component into the catalytic composite involves the utilization of a soluble decomposable compound or complex of bismuth to impregnate the porous carrier material. in general, the solvent used in this impregnation step is selected on the basis of its capability to dissolve the desired bismuth compound and is typically an aqueous acidic solution. Hence, the bismuth component may be added to the carrier material by commingling the latter with an aqueous solution of a suitable bismuth salt or water-soluble compound or complex of bismuth such as bismuth ammonium citrate, bismuth tribromide, bismuth trichloride, bismuth trihydroxide, bismuth oxychloride, bismuth oxybromide, bismuth trioxide, bismuth potassium tartrate, bismuth acetate, bismuth oxycarbonate, bismuth nitrate and the like compounds. Best results are ordinarily ob tained with a solution of bismuth trichloride in hydrochloric acid. In general, the bismuth component can be impregnated either prior to, simultaneously with, or after the other metallic component is added to the carrier material. However, I have obtained excellent results by impregnating the bismuth component simultaneously with the platinum group component. In fact. I have determined that a preferred impregnation solution contains chloroplatinic acid, hydrochloric acid and bismuth trichloride.

Regardless of which bismuth compound is used in the preferred impregnation step, it is important that the bismuth component be uniformly distributed throughout the carrier material. In order to achieve this objective it is necessary to maintain the pH of the impregnation solution at a value less than 3. and preferably less than 1, and to dilute the solution to a volume which is approximately the same or greater than the volume of the carrier material which is impregnated. It is preferred to use a volume ratio of impregnation solution to carrier material of at least 0.75:1 and preferably about 1:1 to about 3:1 or more. Similarly, a relatively long contact time should be uesd during this impregnation step ranging from about 0.25 hours up to about 0.5 hours or more. The carrier material is likewise preferably constantly agitated during this impregnation step.

It is essential to incorporate a halogen component into the bimetallic catalytic composite of the present invention. Although the precise form of the chemistry of the association of the halogen component with the carrier material is not entirely known, it is customary in the art to refer to the halogen component as being combined with the carrier material, or with the other ingredients of the catalyst in the form of the halide (eg. as the combined chloride). This combined halogen may be either fluorine, chlorine, bromine, or mixtures thereof. Of these fluorine and, particularly, chlorine are preferred for the purpose of the present invention. The halogen may be added to the carrier material in any suitable manner, either during preparation of the support or before or after the addition of the other components. For example, the halogen may be added, at any stage of the preparation of the carrier material or to the calcined carrier material, as an aqueous solution of a suitable, decomposable halogen-containing compound such as hydrogen fluoride, hydrogen chloride, hydrogen bromide, ammonium chloride, etc. The halogen component or a portion thereof, may be combined with the carrier material during the impregnation of the latter with the metallic components; for example, through the utilization of a mixture of chloroplatinic acid. bismuth trichloride and hydrogen chloride. In another situation. the alumina hydrosol which is typically utilized to form the preferred alumina carrier material may contain halogen and thus contribute at least a portion of the halogen component to the final composite. For reforming, the halogen will be typically combined with the carrier material in an amount sufficient to result in a final composite that contains about 0.1 to about 3.5% and preferably about 0.5 to about 1.5% by weight of halogen, calculated on an elemental basis. In isomerization or hydrocracking embodiments. it is generally preferred to utilize relatively larger amounts of halogen in the catalyst typically, ranging up to about 10 wt. halogen calculated on an elemental basis, and more preferably about 1 to about 5 wt. 7c.

Regarding the amount of the bismuth component used in the subject catalyst, I have found that it is essential to fix the amount of the bismuth component as a function of the amount of the platinum group component contained in the composite. More specifically, I have observed that the beneficial interaction of the hismuth component with the platinum group component is only obtained when the bismuth component is present, on an atomic basis, in an amount not greater than the platinum group component. Quantitatively, the amount of the bismuth component is preferably sufficient to provide an atomic ratio of bismuth to platinum group metal of about 0.1:1 to about 1:1, with best results obtained at an atomic ratio of about 0. l :1 to about 0.75:1. The criticalness associated with this atomic ratio limitation is apparent when an attempt is made to convert hydrocarbons with a catalyst having an atomic ratio of bismuth to platinum group metal of greater than 1:1. In this latter case, substantial deactivation of the platinum component is observed. Accordingly, it is an essential feature of the present invention that the amount of the bismuth component is chosen as a function of the amount of the platinum group component in order to insure that the atomic ratio of these components in the resulting catalyst is within the stated range. Specific examples of especially preferred catalytic composites are as follows: (I) a catalytic composite comprising 0.375 wtv platinum, 0.2 wt. sulfur, 0.25 wt. bismuth, and 0.5 to 1.5 wt. halogen combined with an alumina carrier material (atomic ratio Bi to Pt 0.62:1); (2) a catalytic composite comprising 0.375 wt. platinum, 0.15 wt. sulfur, 0.15 wt. bismuth. and 0.5 to 1.5 wt. halogen combined with an alumina carrier material (atomic ratio Bi to Pt 0.37:1 (3) a catalytic composite comprising 0.375 wt. Z? platinum, 0.1 wt. sulfur, 0.1 wt. 7r bismuth and 0.5 to 1.5 wt. halogen combined with an alumina carrier material (atomic ratio Bi to Pt 0.25:1); (4) a catalytic composite comprising 0.375 wt. 7c platinum, 0.1 wt. "/r sulfur, 0.05 wt. bismuth and 0.5 to 1.5 wt. 7: halogen combined with an alumina carrier material (atomic ratio Bi to Pt 0.12:1 l", and, (5) a catalytic composite comprising 0.75 wt. We platinum, 0.4 wt. "/c sulfur. 0.4 wt. bismuth and 0.5 to 1.5 wt. "/a halogen combined with an alumina carrier material (atomic ratio Bi to Pt 0.5:1

Another significant parameter for the present catalyst is the total metals content which is defined to be the sum of the platinum group component and the bismuth component, calculated on an elemental basis. Good results are ordinarily obtained with the subject catalyst when this parameter is fixed at a value of about 0.15 to about 2 wt. 7a, with best results ordinarily achieved at a metals loading of about 0.3 to about 1 wt.

An optional ingredient for the bimetallic catalyst of the present invention is a Friedel-Crafts metal halide component. This ingredient is particularly useful in hydrocarbon conversion embodiments of the present invention wherein it is preferred that the catalyst utilized has a strong acid or cracking function associated therewith for example, an embodiment wherein hydrocarbons are to be hydrocracked or isomerized with the catalyst of the present invention. Suitable metal halides of the Friedel-Crafts type include aluminum chloride, aluminum bromide, ferric chloride, ferric bromide, zinc chloride, and the like compounds, with the aluminum halides and particularly aluminum chloride ordinarily yielding best results. Generally. this optional ingredient can be incorporated into the composite of the present invention by any of the conventional methods for adding metallic halides of this type; however, best results are ordinarily obtained when the metallic halide is sublimed onto the surface of the carrier material according to the preferred method disclosed in US. lat. No. 2,999,074. The component can generally be utilized in any amount which is catalytically effective, with a value selected from the range of about 1 to about l0O wt. of the carrier material generally being preferred.

Regardless of the details of how the Components of the catalyst are combined with the porous carrier material. the final catalyst generally will be dried at a temperature of about 200 to about 600 F. for a period of at least about 2 to 24 hours or more, and finally cal cined or oxidized at a temperature of about 700 to about ll00 F. in an air atmosphere for a period of about 0.5 to about 10 hours in order to convert substantially all of the metallic components to the corresponding oxide forms. Because a halogen component is utilized in the catalyst, best results are generally obtained when the halogen content of the catalyst is adjusted during the calcination step by including a halogen or a halogen-containing compound in the air atmo sphere utilized. in particular, when the halogen compo nent of the catalyst is combined chloride, it is preferred to use a mole ratio of H 0 to l-lCl of about 5:l to about 100:1 during at least a portion of the calcination step in order to adjust the final chlorine content of the catalyst to a range of about 0.1 to about 3.5 wt. 7r.

It is an essential feature of the present invention that the resultant oxidized bimetallic catalytic composite is subjected to a substantially water-free reduction step prior to its use in the conversion of hydrocarbons. This step is designed to insure a uniform and finely divided dispersion of the metallic components throughout the carrier material and to selectively reduce the platinum group component and the bismuth component to the corresponding metals. Preferably, substantially pure and dry hydrogen (i.e. less than 20 vol. ppm. H O) is used as the reducing agent in this step. The reducing agent is contacted with the oxidized catalyst at conditions including a temperature of about 800 to about 1200 F., a gas hourly space velocity of about to about 5000 hrf, and a period of time of about 0.5 to 10 hours effective to reduce substantially all of the platinum group component and bismuth component to the elemental metallic state. This reduction treatment may be performed in situ as part of a start-up sequence if precautions are taken to predry the plant to a substantially water-free state and if substantially water-free hydrogen is used.

Another essential feature of the present invention is that the resulting reduced catalytic composite is subjected to a presulfiding operation designed to incorporate in the catalytic composite about 0.05 to about l wt. sulfur, calculated on an elemental basis. in the form of the sulfide. Best results are ordinarily obtained when the amount of sulfur is about 0.05 to about 0.5 wt. 70. Preferably. this presulfiding treatment takes place in the presence of hydrogen and a suitable sulfiding reagent which is a sulfur-containing and metallic sulfide-producing compound such as hydrogen sulfide, disulfides, lower molecular weight mercaptans, organic sulfides, etc. Typically. this procedure comprises treating the selectively reduced catalyst resulting from the reduction step with a sulfiding gas such as a mixture of hydrogen and hydrogen sulfide having about l0 moles of hydrogen per mole of hydrogen sulfide at conditions sufficient to effect the desired incorporation of sulfur, generally including a temperature ranging from about 50 up to about 1 100 F. or more. It is generally a good practice to perform this presulfiding step under substantially water-free conditions. Without the intention of being limited by this explanation, it is believed the interaction between the reduced catalyst and the sulfiding reagent is governed by a physical and/or chemical adsorption mechanism. Thus, the sulfur combined with the reduced catalyst during this sulfiding step is physically adsorbed or chemisorbed on the surface of the catalyst in the form of the sulfide without necessarily changing or substantially modifying the oxidation states of the metallic moieties contained therein.

According to the present invention, a hydrocarbon charge stock and hydrogen are contacted with the sulfided acidic bimetallic catalyst of the present invention in a hydrocarbon conversion Zone. This contacting may be accomplished by using the catalyst in a fixed bed system, a moving bed system, a fluidized bed system, or in a batch type operation; however, in view of the danger of attrition losses of the valuable catalyst, and of well known operational advantages, it is preferred to use a fixed bed system. in this system, a hydrogen-rich gas and the charge stock are preheated by any suitable heating means to the desired reaction temperature and then are passed into a conversion Zone containing a fixed bed of the catalyst type previously characterized. it is. of course, understood that the conversion zone may be one or more separate reactors with suitable means therebetween to insure that the desired conversion tcrnperatureis maintained at the entrance to each reactor. it is also important to note that the reactants may be contacted with the catalyst bed in either upward. downward. or radial flow fashion with the latter being preferred. in addition, the reactants may be in the liquid phase, a mixed liquid-vapor phase. or a vapor phase when they contact the catalyst, with best results obtained in the vapor phase.

In the case where the bimetallic catalyst of the present invention is used in a reforming operation, the re forming system will comprise a reforming zone containing a fixed bed of the catalyst type previously characterized. This reforming zone may be one or more separate reactors with suitable heating means therebctween to compensate for the endothermic nature of the reactions that take place in each catalyst bed. The hydrocarbon feed stream that is charged to this reforming system will comprise hydrocarbon fractions containing naphthenes and paraffins that boil within the gasoline range. The preferred charge stocks are those consisting essentially of naphthenes and paraffins, although in some cases aromatics and/or olefms may also be present. This preferred class includes straight run gasolines, natural gasolines, synthetic gasolines and the like. On the other hand, it is frequently advantageous to charge thermally or catalytically cracked gasolines or higher boiling fractions thereof. Mixtures of straight run and cracked gasolines can also be used to advantage. The gasoline charge stock may be a full boiling gasoline having an initial boiling point of from about 50 to about 150 F. and an end boiling point within the range of from about 325 to about 425 F., or may be a selected fraction thereof which generally will be a higher boiling commonly referred to as a heavy naphtha for example. a naphtha boiling in the range of C to 400 F. In some cases, it is also advantageous to charge pure hydrocarbons or mixtures of hydrocarbons that have been extracted from hydrocarbon distillates for example. straight-chain paraffins which are to be converted to aromatics. It is preferred that these charge stocks be treated by conventional catalytic pretreat ment methods such as hydrorefining, hydrotreating, hy drodesulfurization. etc. to remove substantially all sulfurous. nitrogenous and water-yielding contaminants therefrom and to saturate any olefms that may be contained therein.

In other hydrocarbon conversion embodiments, the charge stock will be of the conventional type customarily used for the particular kind of hydrocarbon conversion being effected. For example. in a typical isom' erization embodiment the charge stock can be a paraffinic stock rich in C, to C normal paraffins, or :2 normal butane-rich stock, or an n-hexane-rich stock, or a mixture of xylene isomers, etc. In a dehydrogenation embodiment, the charge stock can be any of the known dehydrogenatable hydrocarbons such as an aliphatic compound containing 2 to 30 carbon atoms per molecule, a C to C normal paraffin. a C to (I, alkylaromatic, a naphthene and the like. in hydrocracking embodiments, the charge stock will be typically a gas oil, heavy cracked cycle oil. etc. In addition alkylaromatics and naphthenes can be conveniently isomerized by using the catalyst of the present invention. Likewise. pure hydrocarbons or substantially pure hydrocarbons can be converted to more valuable products by using the bimetallic catalysts of the present invention in any of the hydrocarbon conversion processes. known to the art, that use a dual-function catalyst.

in a reforming embodiment, it is generally preferred to utilize the sulfided acidic bimetallic catalytic com posite in a substantially water-free environment. Essential to the achievement of this condition in the reforming zone is the control of the water level present in the charge stock and the hydrogen stream which is being charged to the zone. Best results are ordinarily obtained when the total amount of water entering the conversion zone from any source is held to a level less than 50 ppm. and preferably less than 20 ppm.; expressed as weight of equivalent water in the charge stock. in general. this can be accomplished by careful control of the water present in the charge stock and in the hydrogen stream. The charge stock can be dried by using any suitable drying means known to the art such as a conventional solid adsorbent having a high selec tivity for water; for instance, sodium or calcium crystalline aluminosilicates, silica gel, activated alumina, molecular sieves, anhydrous calcium sulfate, high surface area sodium and the like adsorbent. Similarly. the water content of the charge stock may be adjusted by suitable stripping operations in a fractionation column or like device. And in some cases. a combination of adsorbent drying and distillation drying may be used advantageously to effect almost complete removal of water from the charge stock. Preferably. the charge stock is dried to a level corresponding to less than 20 ppm. of H 0 equivalent. In general, it is preferred to maintain the water content of the hydrogen stream entering the hydrocarbon conversion zone at a level of about 10 to about 20 vol. ppm. of water or less. In the case where the water content of the hydrogen stream is above this range, this can be conveniently accomplished by contacting the hydrogen stream with a suitable desiccant such as those mentioned above at conventional drying conditions.

In the reforming embodiment, an effluent stream is withdrawn from the reforming zone and passed through a cooling means to a separation zone, typically maintained at about 25 to 150 F.. wherein a hydrogen-rich gas is separated from a high octane liquid product. commonly called an unstabilized reformate. When a super-dry operation is desired, at least a portion of this hydrogen-rich gas is withdrawn from the separating zone and passed through an adsorption zone containing an adsorbent selective for water. The resultant substantially water-free hydrogen stream can then be recycled through suitable compressing means back to the reforming zone. The liquid phase from the separating zone is typically withdrawn and commonly treated in a fractionating system in order to adjust the butane concentration, thereby controlling frontend volatility of the resulting reformate.

The conditions utilized in the numerous hydrocarbon conversion embodiments of the present invention are those customarily used in the art for the particular reaction, or combination of reactions, that is to be effected. For instance, alkylaromatics and paraffin isomerization conditions include: a temperature of about 32 to about 1000 F. and preferably about to about 600 F.; a pressure of atmospheric to about atmospheres; a hydrogen to hydrocarbon mole ratio of about 0.5:1 to about 20:1 and a LHSV (calculated on the basis of equivalent liquid volume of the charge stock contacted with the catalyst per hour divided by the volume of conversion zone containing catalyst) of about 0.2 hr. to 10 hr.'. Dehydrogenation conditions include: a temperature of about 700 to about l250 F., a pressure of about 0.1 to about atmospheres, a liquid hourly space velocity of about 1 to 40 hr. and a hydrogen to hydrocarbon mole ratio of about l:l to 20:l. Likewise, typically hydrocracking conditions include: a temperature of about 400 to about 900 F.; a pressure of about 500 psig. to about 3000 psi 21 LHSV of about 0.l hr. to about 10 hr.; and hydro gen circulation rates of about 1000 to 10,000 SCF per barrel of charge.

In the reforming embodiment of the present invention the pressure utilized is selected from the range of about 0 psig. to about 1000 psig., with the preferred pressure being about 50 psig. toabout 600 psig. Particularly good results are obtained at low pressure; namely, a pressure of about 50 to 350 psig. In fact, it is a singular advantage of the present invention tnat it allows stable operation at lower pressure than have heretofore been successfully utilized in so-called continuous reforming systems (i.e. reforming for periods of about to about 200 or more barrels of charge per pound of catalyst without regeneration) with all platinum monometallic catalysts. in other words, the bimetallic catalyst of the present invention allows the operation of a continuous reforming system to be conducted at low pressure (i.e. 100 to about 350 psig.) for about the same or better catalyst life before regeneration as has been heretofore realized with conventional monometallic catalysts at higher pressures (i.e. 400 to 600 psig.). On the other hand, the stability feature of the present invention enables reforming operation conducted at pressures of 400 to 600 psig. to achieve substantially increased catalyst life before regeneration.

Similarly, the temperature required for reforming is generally lower than that required for a similar reforming operation using a high quality catalyst of the prior art. This significant and desirable feature of the present invention is a consequence of the selectivity of the sulfided acidic bimetallic catalyst of the present invention for the octane-upgrading reactions that are preferably induced in a typical reforming operation. Hence the present invention requires a temperature in the range of from about 800 to about l 100 F. and preferably about 900 to about 1050 F. As is well known to those skilled in the continuous reforming art, the initial selection of the temperature within this broad range is made primarily as a function of the desired octane of the product reformate considering the characteristics of the charge stock and of the catalyst. Ordinarily, the temperature then is thereafter slowly increased during the run to compensate for the inevitable deactivation that occurs to provide a constant octane product. Therefore, it is a feature of the present invention that the rate at which the temperature is increased in order to maintain a constant octane product, is substantially lower for the catalyst of the present invention than for a high quality reforming catalyst which is manufactured in exactly the same manner as the catalyst of the present invention except for the inclusion of the bismuth. Moreover, for the catalyst of the present invention, the (3 yield loss for a given temperature increase is substantially lower than for a high quality reforming catalyst of the prior art. In addition, hydrogen production is substantially higher.

The reforming embodiment of the present invention also typically utilizes sufficient hydrogen to provide an amount of about 1 to about moles of hydrogen per mole of hydrocarbon entering the reforming zone, with excellent results being obtained when about 5 to about 10 moles of hydrogen are used per mole of hydrocarbon. Likewise, the liquid hourly space velocity (Ll-iSV) used in reforming is selected from the range of about 0.1 to about 10 hr." ,with a value in the range of about 1 to about 5 hr. being preferred. in fact, it is a feature of the present invention that it allows operations to be conducted at higher LHS'V' than normally can be stably achieved in a continuous reforming process with a high quality reforming catalyst of the prior art. This last feature is of immense economic significance because it allows a continuous reforming process to operate at the same throughput level with less catalyst inventory than that heretofore used with conventional reforming catalysts at no sacrifice in catalyst life before regeneration.

The following working examples are given to illustrate further the preparation of the sulfided acidic bi metallic catalytic composite of the present invention and the use thereof in the conversion of hydrocarbons. it is understood that the examples are intended to be illustrative rather than restrictive.

EXAMPLE I This example demonstrates a particularly good method of preparing the catalytic composite of the present invention.

An alumina carrier material comprising onesixteenth inch spheres is prepared by: forming an aluminum hydroxyl chloride sol by dissolving substantially pure aluminum pellets in hydrochloric acid, adding hexamethylenetetrarnine to the resulting alumina sol, gelling the resulting solution by dropping it into an oil bath to form spherical particles of an aluminumcontaining hydrogel, aging and washing the resulting particles and finally drying and calcining the aged and washed particles to form spherical particles of gammaalumina containing about 0.3 wt. combined chloride. Additional details as to this method of preparing the preferred gamma-alumina carrier material are given in the teachings of U.S. Pat. No. 2,620,314.

An aqueous impregnation solution containing chloroplatinic acid, bismuth trichloride and hydrogen chloride is then prepared. The alumina carrier material is thereafter admixed with the impregnation solution. The amount of reagents contained in this impregnation solution is calculated to result in a final composite containing on an elemental basis, 0.375 wt. platinum and 0.25 wt. bismuth. in order to insure uniform dispersion of the metallic components throughout the carrier material, the amount of hydrochloric acid used is about 3 wt. of the alumina particles. This impregnation step is performed by adding the carrier material particles to the impregnation mixture with constant agitation. In addition, the volume of the solution is approximately the same as the volume of the carrier material particles. The impregnation mixture is maintained in contact with the carrier material particles for a period of about onehalf hour at a temperature of about 70 F. Thereafter, the temperature of the impregnation mixture is raised to about 225 F. and the excess solution evaporated in a period of about 1 hour. The resulting dried particles are then subjected to a calcination or oxidation treatment in air atmosphere at a temperature of about 975 F. for about 1 hour. This oxidation step is designed to convert substantially all of the metallic ingredients to the corresponding oxide forms. The calcined spheres are then contacted with an air stream containing H and l-lCl in a mole ratio of about 30:1 for about 4 hours at 975 F. in order to adjust the halogen content of the catalyst particles to a value of about 1 wt.

The resulting catalyst particles are analyzed and found to contain, on an elemental basis, about 0.375 wt. platinum, about 0.25 wt. bismuth and about 1 wt. combined chloride. For this catalyst the atomic ratio of bismuth to platinum is 0.62:1.

Thereafter, the catalyst particles are subjected to a dry reduction step designed to reduce the platinum and bismuth components to the corresponding elemental metallic states by contacting them for 1 hour with a substantially pure hydrogen stream containing less than 5 vol. ppm. H O at a temperature of about 1050 F., a pressure slightly above atmospheric. and a flow rate of the hydrogen stream through the catalyst particles corresponding to a gas hourly space velocity of about 720 hr..

A gaseous mixture of H and H 8 containing a mole ratio of 1-1 to 1-1 8 of about 10:1 is then contacted with the resulting reduced catalyst at sulfiding conditions, including a temperature of about 1050 F., a gas hourly space velocity of about 700 hr. atmospheric pressure and a contact time of about 1 hour effective to incorporate about 0.2 wt. sulfur in the form of the adsorbed sulfide.

EXAMPLE II A portion of the spherical sulfided acidic bimetallic catalyst particles produced by the method described in Example I are loaded into a scale model of a continuous, fixed bed reforming plant of conventional design. In this plant a heavy Kuwait naphtha and hydrogen are continuously contacted at reforming conditions: a liquid hourly space velocity of 1.5 hr. a pressure of 100 psig., a hydrogen to hydrocarbon mole ratio of 5:1 and a temperature sufficient to continuously produce a C reformate of 102 F-l clear. It is to be noted that these are exceptionally, severe conditions.

The heavy Kuwait naphtha has an API gravity at 60 F. of 60.4, an initial boiling point of 1 84 F., a 50% boiling point of 256 F., and an end boiling point of 360 F. In addition, it contains about 8 vol. aromatics, 71 vol. paraffins, 21 vol. naphthenes, 0.5 wt. parts per million sulfur and 5 to 8 wt. parts per million water. The F-l clear octane number of the raw stock is 40.0

The fixed bed reforming plant is made up of a reactor containing the bimetallic catalyst, a hydrogen separation zone, a debutanizer column, and suitable heating, pumping, cooling and controlling means. In this plant, a hydrogen recycle stream and the charge stock are commingled and heated to the desired temperature. The resultant mixture is then passed downflow into a reactor containing the bimetallic catalyst as a fixed bed. An effluent stream is then withdrawn from the bottom of the reactor, cooled to about 55 F. and passed to a separating zone wherein a hydrogen-rich gaseous phase separates from a liquid hydrocarbon phase. A portion of the gaseous phase is continuously passed through a high surface area sodium scrubber and the resulting water-free hydrogen stream recycled to the reactor in order to supply hydrogen thereto, and the excess hydrogen over that needed for plant pressure is recovered as excess separator gas. The liquid hydrocarbon phase from the hydrogen separating zone is withdrawn therefrom and passed to a debutanizer column of conventional design wherein light ends are taken overhead as debutanizer gas and a C reformate stream recovered as bottoms.

The test run is continued for a catalyst life of about 20 barrels of charge per pound of catalyst utilized, and it is determined that the activity, selectivity and stability of the present sulfided acidic bimetallic catalyst are vastly superior to those observed in a similar type test with a conventional commercial reforming catalyst. More specifically, the results obtained from the subject catalyst are superior to the platinum metal-containing catalyst of the prior art in the areas of hydrogen production, (3 yield at octane, average rate of temperature increase necessary to maintain octane, and C yield decline rate.

It is intended to cover by the following claims all changes and modifications of the above disclosure of the present invention which would be self-evident to a man of ordinary skill in the catalyst formulation art or the hydrocarbon conversion art.

I claim as my invention:

1. A process for reforming a gasoline fraction to produce a high octane reformate which comprises contacting said fraction, at gasoline reforming conditions in the presence of hydrogen with a catalytic composite comprising a porous carrier material containing, on an elemental basis, about 0.01 to about 2 wt. platinum group metal, about 0.05 to about 1 wt. sulfur, about 0.1 to about 3.5 wt. halogen and bismuth in an amount sufficient to result in an atomic ratio of bismuth to platinum group metal of about 0.1:1 to about 1:1, wherein the platinum group metal and bismuth are uniformly dispersed throughout the porous carrier material and wherein substantially all of the platinum group metal and bismuth are present in the corresponding elemental metallic states.

2. A process as defined in claim 1 wherein the platinum group metal is platinum.

3. A process as defined in claim 1 wherein the plati' num group metal is palladium.

4. A process as defined in claim 1 wherein the platinum group metal is iridium.

5. A process as defined in claim 1 wherein the halogen component is combined chloride.

6. A process as defined in claim 1 wherein the porous carrier material is a refractory inorganic oxide.

7. A process as defined in claim 1 wherein the porous carrier material consists essentially of alumina.

8. A process as defined in claim 1 wherein the atomic ratio of bismuth to platinum group metal is about 0. 1 :1 to about 0.75: 1.

9. A process as defined in claim 1 wherein the catalytic composite contains about 0.05 to about 1 wt. platinum group metal, about 0.05 to about 0.5 wt. sulfur, about 0.5 to about 1.5 wt. halogen and an atomic ratio of bismuth to platinum group metal of about 0.1:1 to about 0.75:1.

10. A process as defined in claim 1 wherein substantially all of the sulfur is present therein in the form of physically adsorbed or chemisorbed sulfide.

11. A process as defined in claim 1 wherein the reforming conditions include a temperature of about 800 to 1 F., a pressure of about 0 to about 1000 psig., a liquid hourly space velocity of about 0.1 to about 10 hr." and a mole ratio of hydrogen to hydrocarbon of about 1:1 to about 20:1.

12. A process as defined in claim 1 wherein the contacting step is performed in a substantially water-free environment.

13. A process as defined in claim 1 wherein the reforming conditions include a pressure of about 50 to about 350 psig. 

1. A PROCESS FOR REFORMING A GASOLINE FRACTION TO PRODUCE A HIGH OCTANE REFORMATE WHICH COMPRISES CONTACTING SAID FRACTION, AT GASOLINE REFORMING CONDITIONS IN THE PRESENCE OF HYDROGEN WITH A CATALYTIC COMPOSITE COMPRISING A POROUS CARRIER MATERIAL CONTAINING, ON AN ELEMENTAL BASIS, ABOUT 0.01 TO ABOUT 2 WT. % PLATINUM GROUP METAL, ABOUT 0.05 TO ABOUT 1 WT. % SULFUR, ABOUT 0.1 TO ABOUT 3.5 WT. % HALOGEN AND BISMUTH IN AN AMOUNT SUFFICIENT TO RESULT IN AN ATOMIC RATIO OF BISMUTH TO PLATINUM GROUP METAL OF ABOUT 0.1:1 TO ABOUT 1:1 WHEREIN THE PLATINUM GROUP METAL AND BISMUTH ARE UNIFORMLY DISPERSED THROUGHOUT THE POROUS CARRIER MATERIAL AND WHEREIN SUBSTANTIALLY ALL OF THE PLATINUM GROUP METAL AND BISMUTH ARE PRESENT IN THE CORRESPONDING ELEMENTAL METALLIC STATES.
 2. A process as defined in claim 1 wherein the platinum group metal is platinum.
 3. A process as defined in claim 1 wherein the platinum group metal is palladium.
 4. A process as defined in claim 1 wherein the platinum group metal is iridium.
 5. A process as defined in claim 1 wherein the halogen component is combined chloride.
 6. A process as defined in claim 1 wherein the porous carrier material is a refractory inorganic oxide.
 7. A process as defined in claim 1 wherein the porous carrier material consists essentially of alumina.
 8. A process as defined in claim 1 wherein the atomic ratio of bismuth to platinum group metal is about 0.1:1 to about 0.75:1.
 9. A process as defined in claim 1 wherein the catalytic composite contains about 0.05 to about 1 wt. % platinum group metal, about 0.05 to about 0.5 wt. % sulfur, about 0.5 to about 1.5 wt. % halogen and an atomic ratio of bismuth to platinum group metal of about 0.1:1 to about 0.75:1.
 10. A process as defined in claim 1 wherein substantially all of the sulfur is present therein in the form of physically adsorbed or chemisorbed sulfide.
 11. A process as defined in claim 1 wherein the reforming conditions include a temperature of about 800* to 1100* F., a pressure of about 0 to about 1000 psig., a liquid hourly space velocity of about 0.1 to about 10 hr. 1 and a mole ratio of hydrogen to hydrocarbon of about 1:1 to about 20:1.
 12. A process as defined in claim 1 wherein the contacting step is performed in a substantially water-free environment.
 13. A process as defined in claim 1 wherein the reforming conditions include a pressure of about 50 to about 350 psig. 